Reforming process for renewable aviation fuel

ABSTRACT

Methods of making highly renewable aviation fuel are described. In one embodiment, the method includes reacting a renewable feedstock in a reaction zone to form a mixture of n-paraffins and isomerized paraffins. The mixture of n-paraffins and isomerized paraffins is separated into at least a heavy SPK fraction, and a light SPK fraction. A portion of the light SPK fraction is reformed in a reforming zone under reforming conditions to form a mixture of renewable aromatics. A portion of the mixture of renewable aromatics is mixed into the light SPK fraction, the heavy SPK fraction, an aviation fuel made from a renewable feedstock, or combinations thereof to form the highly renewable aviation fuel component.

FIELD OF THE INVENTION

This invention relates to a process for producing aviation fuel boilingrange hydrocarbons useful as aviation fuel from renewable feedstockssuch as the glycerides and free fatty acids found in materials such asplant oils, animal oils, animal fats, and greases. The process involvesreforming n-paraffin and isomerized reaction products to form a mixtureof aromatics, and mixing the aromatics into a renewable aviation fuelproduct.

BACKGROUND OF THE INVENTION

As the demand for fuels such as aviation fuel increases worldwide, thereis increasing interest in sources other than petroleum crude oil forproducing the fuel. One source is renewable feedstocks including, butnot limited to, plant oils such as corn, jatropha, camelina, rapeseed,canola, soybean and algal oils, animal fats such as tallow, fish oils,and various waste streams such as yellow and brown greases and sewagesludge. The common feature of these feedstocks is that they are composedof mono- di- and tri-glycerides, and free fatty acids (FAA). Anotherclass of compounds appropriate for these processes is fatty acid alkylesters (FAAE), such as fatty acid methyl ester (FAME) or fatty acidethyl ester (FAEE). These types of compounds contain aliphatic carbonchains generally having from about 8 to about 24 carbon atoms. Thealiphatic carbon chains in the glycerides, FFAs, or FAAEs can besaturated or mono-, di- or poly-unsaturated. Most of the glycerides inthe renewable feed stocks will be triglycerides, but some may bemonoglycerides or diglycerides. The monoglycerides and diglycerides canbe processed along with the triglycerides.

There are references disclosing the production of hydrocarbons fromoils. For example, U.S. Pat. No. 4,300,009 discloses the use ofcrystalline aluminosilicate zeolites to convert plant oils (e.g., cornoil) to hydrocarbons (e.g., gasoline), and chemicals (e.g.,para-xylene). U.S. Pat. No. 4,992,605 discloses the production ofhydrocarbon products in the diesel boiling range by hydroprocessingvegetable oils such as canola or sunflower oil. Finally, US 2004/0230085A1 discloses a process for treating a hydrocarbon component ofbiological origin by hydrodeoxygenation followed by isomerization.

SUMMARY OF THE INVENTION

One aspect of the present invention relates to a method of making highlyrenewable aviation fuel component. In one embodiment, the methodincludes reacting a renewable feedstock in a reaction zone to form amixture of n-paraffins and isomerized paraffins. The mixture ofn-paraffins and isomerized paraffins is separated into at least a heavySPK fraction, and a light SPK fraction. A portion of the light SPKfraction is reformed in a reforming zone under reforming conditions toform a mixture of renewable aromatics. A portion of the mixture ofrenewable aromatics is mixed into the light SPK fraction, the heavy SPKfraction, an aviation fuel made from a renewable feedstock, orcombinations thereof to form the highly renewable aviation fuelcomponent.

BRIEF DESCRIPTION OF THE DRAWING

The Figure is a general flow schematic of one embodiment of a process.

DETAILED DESCRIPTION OF THE INVENTION

Renewable aviation fuel is currently made by hydroprocessing renewablefeedstocks to produce aviation range hydrocarbons. This product is knownas synthetic paraffinic kerosene (SPK). The process also producesparaffinic green diesel, paraffinic green naphtha, and liquefiedpetroleum gas (LPG). In a second stage of the process, the n-paraffinsare isomerized and mildly cracked to improve the cold properties of theresulting paraffins.

SPK typically cannot meet the commercial specifications for density foraviation fuel, so the SPK is blended with aviation range aromatics toobtain a blended fuel meeting the density specification. The aviationrange aromatics are currently not derived from renewable sources, butare conventional fossil fuel derived aromatics. Because of therequirement for high quality aromatics in the aviation fuel boilingrange, aviation fuel from 100% plant and animal oils is difficult tomake.

In the present process, the SPK is subjected to a reforming process toproduce aviation range aromatics. The aviation range aromatics can thenbe blended with another portion of SPK or a separate SPK stream to makean aviation fuel component meeting the necessary specifications. Theaviation range aromatics are generally about 5 wt % to about 25 wt % ofthe aviation fuel component, or about 8 wt % to about 25 wt %. Becausethe aviation range aromatics are derived from a renewable feedstock, theresulting aviation fuel component is highly renewable. By aviation fuelcomponent, we mean any component that can be blended to produce aviationfuel, up to and including the resulting aviation fuel itself (e.g., whenblended with a petroleum based aviation fuel). By highly renewable, wemean that at least about 25 wt % of the total aromatics used in anaviation fuel component are derived from a renewable feedstock, or atleast about 50 wt %, or at least about 75 wt %, or at least about 80 wt%, or at least about 90 wt %, or at least about 95 wt %.

The naphtha product from the process described above is very paraffinicand low octane. Optionally, a portion of the green naphtha can be alsobe subjected to the reforming process to make naphtha range aromatics,which can then be blended with the green naphtha to make high-octanegreen naphtha.

One embodiment of the process is illustrated in the Figure. Therenewable feedstock 5 enters the reaction zone 10. The reaction zone 10includes one or more zones for one or more of hydrotreating,isomerization, and hydrocracking. The effluent 15 from the reaction zone10 includes a mixture of n-paraffins and isoparaffins. The effluent 15is sent to a stripping column 20. The overheads 25 from the strippingcolumn 20 is exported from the unit as LPG or fuel gas. The bottoms 30from the stripping column 20 is sent to a fractionator 35 where it isseparated into different streams which can include at least one or moreof a green naphtha fraction 40, a light SPK fraction 45, a heavy SPKfraction 50, and a green diesel faction 55.

In some embodiments, the light SPK fraction 45 is split into twoportions 45A and 45B. Light SPK fraction 45A is sent to reformer 60. Inother embodiments, the entire light SPK fraction 45 is sent to thereformer. In some embodiments, all or a portion 40A of the green naphthafraction 40 is also sent to reformer 60.

The light SPK fraction 45A and green naphtha fraction 40A (if present)are reformed in reformer 60. The reformer conditions typically include atemperature in the range of about 300° C. to about 520° C., or about410° C. to about 500° C., or about 380° C. to about 470° C., a pressurein the range of about 345 kPa (about 50 psig) to about 2758 kPa (about400 psig), or about 1034 kPa (about 150 psig) to about 2068 kPa (about300 psig), and a ratio of H₂:HC of about 0.5 to about 10, or about 2 toabout 8.

The effluent 65 from the reformer 60 includes aviation range aromatics,and naphtha range aromatics if a green naphtha fraction was reformed, aswell as hydrogen. The effluent 65 is separated in a separator 70 into ahydrogen stream 75 and a liquid stream 80 including the aviation rangearomatics and the naphtha range aromatics. The hydrogen stream 75 can berecycled back to the reaction section 10 and/or reformer 60, if desired.The liquid stream 80 is sent to fractionator 85 where the aviation rangearomatics 90 are separated from the naphtha range aromatics 95.

The aviation range aromatics 95 can be combined with one or more of thelight SPK fraction 45B, the heavy SPK fraction 50, and a stream ofrenewable aviation fuel made in a separate process to form a highlyrenewable aviation fuel.

In some embodiments, the naphtha range aromatics 95 can be combined withthe naphtha fraction 40 to make high octane green gasoline.

In some embodiments, the green diesel fraction 55 can be recovered.

The term renewable feedstock is meant to include feedstocks other thanthose obtained directly from petroleum crude oil. Another term that hasbeen used to describe this class of feedstocks is renewable fats andoils. The renewable feedstocks that can be used in the present inventioninclude any of those which comprise glycerides and free fatty acids(FFA). Examples of these feedstocks include, but are not limited to,canola oil, corn oil, soy oils, rapeseed oil, soybean oil, colza oil,tall oil, sunflower oil, hempseed oil, olive oil, linseed oil, coconutoil, castor oil, peanut oil, palm oil, mustard oil, cottonseed oil,tallow, yellow and brown greases, lard, train oil, fats in milk, fishoil, algal oil, sewage sludge, cuphea oil, camelina oil, jatropha oil,curcas oil, babassu oil, palm kernel oil, crambe oil, and the like.Biorenewable is another term used to describe these feedstocks. Theglycerides, FFAs, and fatty acid alkyl esters, of the typical vegetableoil or animal fat contain aliphatic hydrocarbon chains in theirstructure which have about 8 to about 24 carbon atoms with a majority ofthe oils containing high concentrations of fatty acids with 16 and 18carbon atoms. Mixtures or co-feeds of renewable feedstocks and fossilfuel derived hydrocarbons may also be used as the feedstock. Otherfeedstock components may be used if the carbon chain length iswell-defined before mixing with renewable oils to allow meeting desiredyields and specifications for diesel and aviation range paraffins.

Various additives may be combined with the aviation fuel compositiongenerated in order to meet required specifications for differentspecific fuels. The specifications could include physicalcharacteristics, chemical characteristics, or both. The specificationscould be industry standard, government, and/or military fuel standardspecifications. In particular, the hydrocarbon product stream in theaviation fuel range generated herein complies with, is a blendingcomponent for, or may be combined with one or more additives to meet atleast one of: ASTM D 7566 Specification for Aviation Turbine FuelContaining Synthesized Hydrocarbons, ASTM D 1655 Specification forAviation Turbine Fuels Defense Stan 91-91 Turbine Fuel, AviationKerosene Type, Jet A-1 NATO code F-35, F-34, F-37 Aviation Fuel QualityRequirements for Jointly Operated Systems (Joint Checklist) Acombination of ASTM and Def Stan requirements GOST 10227 Jet FuelSpecifications (Russia) Canadian CAN/CGSB-3.22 Aviation Turbine Fuel,Wide Cut Type Canadian CAN/CGSB-3.23 Aviation Turbine Fuel, KeroseneType MIL-DTL-83133, JP-8, MW-DTL-5624, JP-4, JP-5 QAV-1 (Brazil)Especifcacao de Querosene de Aviacao No. 3 Jet Fuel (Chinese) accordingto GB6537 DCSEA 134A (France) Carbureacteur Pour TurbomachinesD'Aviation, Type Kerosene Aviation Turbine Fuels of other countries,meeting the general grade requirements for Jet A, Jet A-1, Jet B, andTS-1 fuels as described in the IATA Guidance Material for AviationTurbine Fuel Specifications. Additives may be added to the jet fuel inorder to meet particular specifications. One particular type of jet fuelis JP-8, defined by Military Specification ML-DTL-83133, which is amilitary grade type of highly refined kerosene based jet propellantspecified by the United States Government.

Renewable feedstocks that can be used in the present invention maycontain a variety of impurities. For example, tall oil is a byproduct ofthe wood processing industry, and it contains esters and rosin acids inaddition to FFAs. Rosin acids are cyclic carboxylic acids. The renewablefeedstocks may also contain contaminants such as alkali metals, e.g.sodium and potassium, phosphorous, as well as solids, water anddetergents. An optional first step is to remove as much of thesecontaminants as possible. Any known pretreatment steps can be usedincluding, but not limited to, contacting the renewable feedstock withan ion-exchange resin in a pretreatment zone at pretreatment conditions,contacting the renewable feedstock with a bleaching earth, such asbentonite clay, in a pretreatment zone, mild acid washing, the use ofguard beds, filtration and solvent extraction techniques,hydroprocessing, such as that described in U.S. application Ser. No.11/770,826, hydrolysis may be used to convert triglycerides to acontaminant mixture of free fatty acids, and hydrothermolysis may beused to convert triglycerides to oxygenated cycloparaffins, orcombinations thereof.

The renewable feedstocks are flowed to a reaction zone or stagecomprising one or more catalyst beds in one or more reactor vessels.Within the reaction zone or stage, multiple beds or vessels may beemployed, and where multiple beds or vessels are employed, interstageproduct separation may or may not be performed between the beds orvessels. The term feedstock is meant to include feedstocks that have notbeen treated to remove contaminants, as well as those feedstockspurified in a pretreatment zone or an oil processing facility. Therenewable feedstocks, with or without additional liquid recycled fromone or more product streams, may be mixed in a feed tank upstream of thereaction zone, mixed in the feed line to the reactor, or mixed in thereactor itself. In the reaction zone, the renewable feedstocks arecontacted with a multifunctional catalyst or set of catalysts comprisingdeoxygenation, hydrogenation, and isomerization functions in thepresence of hydrogen.

A number of reactions occur concurrently within the reaction zone. Theorder of the reactions is not critical to the invention, and thereactions may occur in various orders. One reaction occurring in thereaction zone is hydrogenation to saturate olefinic compounds in thereaction mixture. Another type of reaction occurring in the reactionzone is deoxygenation. The deoxygenation of the mixture may proceedthrough different routes such as decarboxylation, where the feedstockoxygen is removed as carbon dioxide, decarbonylation, where thefeedstock oxygen is removed as carbon monoxide, and/orhydrodeoxygenation, where the feedstock oxygen is removed as water.Decarboxylation, decarbonylation, and hydrodeoxygenation are hereincollectively referred to as deoxygenation reactions.

Sufficient isomerization to prevent poor cold flow properties is needed.Aviation fuel and aviation blending components must have better coldflow properties than is achievable with essentially all n-paraffins, andanother reaction occurring in the reaction zone is isomerization toisomerize at least a portion of the n-paraffins to branched paraffins.The yield of isomerization needed is dependent on the specificationsrequired for the final fuel product. Some fuels require a lower cloud orfreeze point, and thus need a greater yield from the isomerizationreaction to produce a larger concentration of branched-paraffins.Alternatively, depending on the product properties targeted, and theblend of feedstocks used, the isomerization step may not be absolutelynecessary.

As mentioned above, the multifunctional catalyst or set of catalystscomprise deoxygenation, hydrogenation, and isomerization functions. Thecatalyst function for deoxygenation and hydrogenation will be similar tothose already known for hydrogenation or hydrotreating. Thedeoxygenation and hydrogenation functions, which may be the same orseparate active sites, may be noble metals such as a platinum groupmetals including but not limited to ruthenium, rhodium, palladium,platinum, and mixtures thereof, supported on a high surface area carriermaterial such as alumina, silica, silica-alumina, magnesium oxide,titania, zirconia, activated carbon and others known in the art, atlevels ranging from about 0.05 to about 10 weight-% of the catalyticcomposite. Examples of other active sites that may be employed toprovide the deoxygenation and hydrogenation functions are sulfided basemetals such as sulfided NiMo or sulfided NiW. A base metal is a metalwhich oxidizes when heated in air, and other base metals, in addition tonickel, molybdenum and tungsten, which may be a catalyst componentherein include iron, lead, zinc, copper, tin, germanium, chromium,titanium, cobalt, rhenium, indium, gallium, uranium, dysprosium,thallium and mixtures and compounds thereof. Sulfided base metalcatalysts may optionally be supported on carrier material such asalumina, silica, silica-alumina, magnesium oxide, activated carbon andothers known in the art, or may alternately be used without additionalsupport components,

Catalyst functions and conditions for isomerization are well known inthe art. See for example US 2004/0230085 A1 which is incorporated byreference in its entirety. Due to the presence of hydrogen, thesereactions may also be called hydroisomerization.

Overall, the isomerization of the paraffinic product can be accomplishedin any manner known in the art or by using any suitable catalyst knownin the art. In general, catalysts or catalytic components having an acidfunction and mild hydrogenation function are favorable for catalyzingthe isomerization reaction. For a single multi-component catalyst, thesame active site employed for deoxygenation can also serve as the mildhydrogenation function for the isomerization reactions. In general,suitable isomerization catalysts comprise a metal of Group VIII (IUPAC8-10) of the Periodic Table and a support material. Suitable Group VIIImetals include platinum and palladium, each of which may be used aloneor in combination. The support material may be amorphous or crystalline,or a combination of the two. Suitable support materials include,aluminas, amorphous aluminas, amorphous silica-aluminas, ferrierite,ALPO-31, SAPO-11, SAPO-31, SAPO-37, SAPO-41, SM-3, MgAPSO-31, FU-9,NU-10, NU-23, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-50, ZSM-57,MeAPO-11, MeAPO-31, MeAPO-41, MgAPSO-11, MgAPSO-31, MgAPSO-41,MgAPSO-46, ELAPO-11, ELAPO-31, ELAPO-41, ELAPSO-11, ELAPSO-31,ELAPSO-41, laumontite, cancrinite, offretite, hydrogen form ofstillbite, magnesium or calcium form of mordenite, and magnesium orcalcium form of partheite, each of which may be used alone or incombination. ALPO-31 is described in U.S. Pat. No. 4,310,440. SAPO-11,SAPO-31, SAPO-37, and SAPO-41 are described in U.S. Pat. No. 4,440,871.SM-3 is described in U.S. Pat. Nos. 4,943,424; 5,087,347; 5,158,665; andU.S. Pat. No. 5,208,005. MgAPSO is a MeAPSO, which is an acronym for ametal aluminumsilicophosphate molecular sieve, where the metal Me ismagnesium (Mg). Suitable MgAPSO-31 catalysts include MgAPSO-31. MeAPSOsare described in U.S. Pat. No. 4,793,984, and MgAPSOs are described inU.S. Pat. No. 4,758,419. MgAPSO-31 is a preferred MgAPSO, where 31 meansa MgAPSO having structure type 31. Many natural zeolites, such asferrierite, that have an initially reduced pore size can be converted toforms suitable for isomerization by removing associated alkali metal oralkaline earth metal by ammonium ion exchange and calcination to producethe substantially hydrogen form, as taught in U.S. Pat. No. 4,795,623and U.S. Pat. No. 4,924,027. Further catalysts and conditions forskeletal isomerization are disclosed in U.S. Pat. Nos. 5,510,306,5,082,956, and U.S. Pat. No. 5,741,759.

The isomerization catalyst function may also comprise a modifierselected from the group consisting of lanthanum, cerium, praseodymium,neodymium, phosphorus, samarium, gadolinium, terbium, and mixturesthereof, as described in U.S. Pat. No. 5,716,897 and U.S. Pat. No.5,851,949. Other suitable support materials include ZSM-22, ZSM-23, andZSM-35, which are described for use in dewaxing in U.S. Pat. No.5,246,566 and in the article entitled “New molecular sieve process forlube dewaxing by wax isomerization,” written by S. J. Miller, inMicroporous Materials 2 (1994) 439-449. The teachings of U.S. Pat. Nos.4,310,440; 4,440,871; 4,793,984; 4,758,419; 4,943,424; 5,087,347;5,158,665; 5,208,005; 5,246,566; 5,716,897; and U.S. Pat. No. 5,851,949are hereby incorporated by reference.

U.S. Pat. No. 5,444,032 and U.S. Pat. No. 5,608,968 teach a suitablebifunctional catalyst which is constituted by an amorphoussilica-alumina gel and one or more metals belonging to Group VIIIA, andis effective in the hydroisomerization of long-chain normal paraffinscontaining more than 15 carbon atoms. U.S. Pat. Nos. 5,981,419 and5,908,134 teach a suitable bifunctional catalyst which comprises: (a) aporous crystalline material isostructural with beta-zeolite selectedfrom boro-silicate (BOR-B) and boro-alumino-silicate (Al-BOR-B) in whichthe molar SiO₂:Al₂O₃ ratio is higher than 300:1; (b) one or moremetal(s) belonging to Group VIIIA, selected from platinum and palladium,in an amount comprised within the range of from 0.05 to 5% by weight.Article V. Calemma et al., App. Catal. A: Gen., 190 (2000), 207 teachesyet another suitable catalyst.

While at least one exemplary embodiment has been presented in theforegoing detailed description of the invention, it should beappreciated that a vast number of variations exist. It should also beappreciated that the exemplary embodiment or exemplary embodiments areonly examples, and are not intended to limit the scope, applicability,or configuration of the invention in any way. Rather, the foregoingdetailed description will provide those skilled in the art with aconvenient road map for implementing an exemplary embodiment of theinvention. It being understood that various changes may be made in thefunction and arrangement of elements described in an exemplaryembodiment without departing from the scope of the invention as setforth in the appended claims.

What is claimed is:
 1. A method of making highly renewable aviation fuelcomponent comprising: reacting a renewable feedstock in a reaction zoneto form a mixture of n-paraffins and isomerized paraffins; separatingthe mixture of n-paraffins and isomerized paraffins into at least aheavy SPK fraction, and a light SPK fraction; reforming a portion of thelight SPK fraction in a reforming zone under reforming conditions toform a mixture of renewable aromatics; mixing a portion of the mixtureof renewable aromatics into the light SPK fraction, the heavy SPKfraction, an aviation fuel made from a renewable feedstock, orcombinations thereof to form the highly renewable aviation fuelcomponent.
 2. The method of claim 1 wherein separating the mixture ofn-paraffins and isomerized paraffins further comprises separating themixture of n-paraffins and isomerized paraffins into a naphtha fraction,and further comprising reforming a first portion of the naphtha fractionwith the portion of the light SPK fraction to form the mixture ofrenewable aromatics.
 3. The method of claim 2 further comprisingseparating the mixture of renewable aromatics into an aviation rangerenewable aromatic fraction and a naphtha range renewable aromaticfraction; and wherein mixing the portion of the mixture of renewablearomatics into the light SPK fraction, the heavy SPK fraction, theaviation fuel component made from the renewable feedstock, orcombinations thereof comprises mixing the aviation range renewablearomatic fraction into the light SPK fraction, the heavy SPK fraction,the aviation fuel component made from the renewable feedstock, orcombinations thereof
 4. The method of claim 3 further comprising mixingthe naphtha range renewable aromatic fraction with a second portion ofthe naphtha fraction, an additional naphtha stream, or combinationsthereof
 5. The method of claim 1 wherein reacting the renewablefeedstock in the reaction zone to form the mixture of n-paraffins andisomerized paraffins comprises: hydrotreating the renewable feedstock ina hydrotreating zone under hydrotreating conditions to obtain a mixtureof n-paraffins; and isomerizing at least a portion of the n-paraffins inan isomerization zone under isomerization conditions to obtain themixture of n-paraffins and isomerized paraffins.
 6. The method of claim1 further comprising recycling hydrogen formed in reforming to thereaction zone or the reforming zone.
 7. The method of claim 1 whereinthe reforming conditions comprise a temperature in a range of about 300°C. to about 520° C., a pressure in a range of about 345 kPa (about 50psig) to about 2758 kPa (about 400 psig), and a ratio of H₂:HC of about0.5 to about
 10. 8. The method of claim 1 wherein the reformingconditions comprise a temperature in a range of about 410° C. to about500° C., a pressure in a range of about 1034 kPa (about 150 psig) toabout 2068 kPa (about 300 psig), and a ratio of H₂:HC of about 2 toabout
 8. 9. The method of claim 1 wherein the reforming takes place inthe presence of a noble metal catalyst.
 10. The method of claim 1wherein the highly renewable aviation fuel component comprises about 8wt % to about 25 wt % renewable aromatics.
 11. The method of claim 1wherein the portion of the mixture of aromatics comprises at least about25 wt % of a total of aromatics in the highly renewable aviation fuelcomponent.
 12. A method of making highly renewable aviation fuelcomponent comprising: hydrotreating the renewable feedstock in ahydrotreating zone under hydrotreating conditions to obtain a mixture ofn-paraffins; and isomerizing at least a portion of the n-paraffins in anisomerization zone under isomerization conditions to obtain the mixtureof n-paraffins and isomerized paraffins; separating the mixture ofn-paraffins and isomerized paraffins into at least a heavy SPK fraction,and a light SPK fraction; reforming a portion of the light SPK fractionin a reforming zone under reforming conditions to form a mixture ofrenewable aromatics; mixing a portion of the mixture of renewablearomatics into the light SPK fraction, the heavy SPK fraction, anaviation fuel made from a renewable feedstock, or combinations thereofto form the highly renewable aviation fuel component.
 13. The method ofclaim 12 wherein separating the mixture of n-paraffins and isomerizedparaffins further comprises separating the mixture of n-paraffins andisomerized paraffins into a naphtha fraction, and further comprisingreforming a first portion of the naphtha fraction with the portion ofthe light SPK fraction to form the mixture of renewable aromatics. 14.The method of claim 13 further comprising separating the mixture ofrenewable aromatics into a aviation range renewable aromatic fractionand a naphtha range renewable aromatic fraction; and wherein mixing theportion of the mixture of renewable aromatics into the light SPKfraction, the heavy SPK fraction the aviation fuel component made fromthe renewable feedstock, or combinations thereof comprises mixing theaviation range renewable aromatic fraction into the light SPK fraction,the heavy SPK fraction, the aviation fuel component made from therenewable feedstock, or combinations thereof
 15. The method of claim 14further comprising mixing the naphtha range renewable aromatic fractionwith a second portion of the naphtha fraction, an additional naphthastream, or combinations thereof
 16. The method of claim 12 furthercomprising recycling hydrogen formed in reforming to the hydrotreatingzone, the isomerization zone, or the reforming zone.
 17. The method ofclaim 12 wherein the reforming conditions comprise a temperature in arange of about 300° C. to about 520° C., a pressure in a range of about345 kPa (about 50 psig) to about 2758 kPa (about 400 psig), and a ratioof H₂:HC of about 0.5 to about
 10. 18. The method of claim 12 whereinthe reforming conditions comprise a temperature in a range of about 410°C. to about 500° C., a pressure in a range of about 1034 kPa (about 150psig) to about 2068 kPa (about 300 psig), and a ratio of H₂:HC of about2 to about
 8. 19. The method of claim 12 wherein the reforming takesplace in the presence of a noble metal catalyst.
 20. The method of claim12 wherein the highly renewable aviation fuel component comprises about5 wt % to about 25 wt % renewable aromatics.